CN107445790A - A kind of energy-saving crude butadiene pre-separation technique - Google Patents
A kind of energy-saving crude butadiene pre-separation technique Download PDFInfo
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- CN107445790A CN107445790A CN201710817736.1A CN201710817736A CN107445790A CN 107445790 A CN107445790 A CN 107445790A CN 201710817736 A CN201710817736 A CN 201710817736A CN 107445790 A CN107445790 A CN 107445790A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
Abstract
The present invention relates to a kind of energy-saving crude butadiene pre-separation technique, it sends to pre-separation tank after specifically including generation air pressure contracting precooling, tank deck gas phase sends to oil-absorption tower and desorber, desorb column overhead or side take-off crude butadiene, pre-separation tank tank bottom liquid phase is respectively after stripper and the separation of crude butadiene knockout tower, the Butadiene Extraction unit for sending to downstream together with after the crude butadiene mixing obtained from desorber from the crude butadiene that crude butadiene separation column overhead obtains further is separated, and the component than carbon quadruple produces from crude butadiene knockout tower tower reactor.Compared with prior art, the present invention uses energy-saving crude butadiene pre-separation technique, the crude butadiene of pre-separation tank tank deck extraction about 30% goes to carry out oily absorption and desorption, the crude butadiene of tank bottom extraction about 70% carries out conventional distillation, comprehensive energy consumption reduces about 16.9% than existing isolation technics, and solve the problems, such as to absorb oil loss, there is significant economic benefit.
Description
Technical field
The present invention relates to the oily absorption and desorption separation technology field of Oxidative Dehydrogenation of Butene into Butadiene separating technology, especially
It is related to a kind of energy-saving crude butadiene pre-separation technique.
Background technology
Butadiene is important basic petrochemical raw material, for produce synthetic rubber, synthetic resin, adiponitrile, oneself two
Amine, nylon66 fiber, sulfolane, 1,4- butanediols etc..The production method of butadiene has C-4-fraction separation and synthetic method (including butane
Dehydrogenation, butylene dehydrogenation, butylene oxidation-dehydrogenation etc.) two kinds.Countries in the world butadiene almost all is directly from hydrocarbon cracking second
Production C-4-fraction during alkene.It is a supplement in butadiene source by butylene oxidation-dehydrogenation technique productions butadiene.In fourth
In alkene oxidative dehydrogenation process production Butadiene Extraction Process, crude butadiene is separated from generation gas by oily absorption and desorption technique
The important unit operation for ensureing butadiene production, the energy consumption of separation and absorb oil consumption be also influence butadiene production into
One of this key factor, so the energy-saving problem of oily absorption and desorption process is increasingly valued by people.
Fig. 1 is a kind of three widely used at present tower oil absorption and desorption techniques, and three towers are oil-absorption tower, desorber and solvent
Oil regeneration tower.The fixed gas in generation gas is removed by oil-absorption tower, fixed gas discharges after vent gas treatment and removes air, and oil is inhaled
Receive tower reactor rich oil and obtain crude butadiene by desorber separation crude butadiene and lean absorption oil, side line, desorb column overhead fixed gas
Return to generation air compressor, the oil-poor recycling of tower reactor.Tower reactor is oil-poor simultaneously 10% sends to solvent naphtha regenerator and is regenerated.
Although this method technology maturation, energy consumption is higher, and it is larger to absorb oil loss.
The Patents of butylene oxidation-dehydrogenation reaction generation gas disposal have CN201310392131, CN201210352538
Deng.The handling process of the disclosed processing butylene oxidation-dehydrogenation reaction generation gas of these patents is the oil suction using traditional three-column process flow
Desorption technique is received, i.e., comprising oil-absorption tower, desorber and solvent naphtha regenerator.By analyzing its technological process, find
Traditional oily absorption and desorption technique has the following disadvantages：
(1) high energy consumption.In three traditional tower oil absorption and desorption techniques, generation gas after compression is all with 40 DEG C of temperature
Oil-absorption tower tower reactor is delivered to, in order to which the component of the carbon such as butadiene four is separated, it is necessary to be absorbed using substantial amounts of from generation gas
Oil, the rich oil of oil-absorption tower kettle desorb in desorber, desorb tower reactor it is oil-poor after pump pressurizes through a series of heat exchange
Device is cooled to about 0 DEG C of return oil-absorption tower top.So, the amount of cyclic absorption oil is bigger, and the consumption of public work is bigger.
(2) it is big to absorb oil loss.Because oxidative dehydrogenation can produce the heavy hydrocarbons such as part benzene, toluene, if these heavy hydrocarbons
It can not be separated, will be dissolved in absorption oil before oily absorption and desorption workshop section.Conventional absorption is mainly carbon six, carbon seven
Deng mixing chain hydrocarbon, the boiling point and benzene, toluene under these chain hydrocarbon normal pressures are very close, are difficult by these using common rectification process
Heavy constituent and absorption oil separation.So, generating the heavy constituent in gas can be accumulated in absorption oil for a long time, and this can substantially reduce absorption
The assimilation effect of oil, in order to reach assimilation effect, gesture necessary complement more absorbs, or even replaces and absorb oil, and this can increase dress
The running cost put.
The content of the invention
It is an object of the present invention to overcome the above-mentioned drawbacks of the prior art and provide a kind of energy-saving cymogene two
Alkene pre-separation technique.
The purpose of the present invention can be achieved through the following technical solutions：
A kind of energy-saving crude butadiene pre-separation technique, comprises the following steps：
(1) after generating the compressed cooling of gas, the separation of pre-separation tank is delivered to, wherein, tank deck gas phase is sent into oil-absorption tower tower reactor,
And the oil of the absorption with entering from oil-absorption tower tower top contacts absorption；
(2) oil-absorption tower top gaseous phase fixed gas one sends to exhaust gas processing device, and Analytic Tower is sent into after the heating of tower reactor rich oil
Middle part；
(3) the gas phase fixed gas two of overhead extraction converges and recycled with generation gas in Analytic Tower, tower reactor extraction it is oil-poor
It is sent to after cooling at the top of oil-absorption tower, side take-off crude butadiene is sent to follow-up BEU；
(4) pre-separation tank tank bottom liquid phase is sent to stripper, and the top gas phase of stripper top extraction returns to converge with generation gas
Conjunction is recycled, and crude butadiene knockout tower is sent to after the heating of tower bottoms heat phase；
(5) crude butadiene knockout tower overhead extraction crude butadiene mixes latter same with the crude butadiene of Analytic Tower side take-off
It is sent to follow-up BEU, tower reactor extraction heavy distillat discharge.
Preferably, the oil-poor and rich oil of oil-absorption tower tower reactor of Analytic Tower tower reactor extraction exchanges heat simultaneously in entry/exit material heat exchanger
Cooling and heating are realized respectively, and the extraction of Analytic Tower tower reactor is oil-poor after the heat exchange cooling of entry/exit material heat exchanger, also by oil-poor
Cooler cools down.
Preferably, the operating pressure of described pre-separation tank is 400kPa~3000kPa, operation temperature be 273.15K~
343.15K.It is furthermore preferred that the operating pressure of described pre-separation tank is 800kPa~1800kPa, operation temperature 273.15K
~313.15K.
Preferably, the mass percent concentration of the component of carbon four of described pre-separation tank tank bottom liquid phase be 70.0~
99.9wt%.It is furthermore preferred that the mass percent concentration of the described component of carbon four is 90.0~99.9wt%.
Preferably, the operating pressure in described stripper is 200kPa~2000kPa, operation temperature be 273.15K~
400.15K.It is furthermore preferred that the operating pressure in described stripper is 500kPa~1000kPa, tower reactor operation temperature is
313.15K~363.15K.
Preferably, the reflux ratio of described crude butadiene knockout tower be 0.3~2, operating pressure be 200kPa~
1000kPa, operation temperature are 273.15K~430K.It is furthermore preferred that the reflux ratio of described crude butadiene knockout tower be 0.5~
1.2, operating pressure is 400kPa~800kPa.
Preferably, described generation gas is butylene oxidation-dehydrogenation reaction generation gas.
Compared with prior art, the present invention has advantages below：
(1) energy consumption is low：Energy-saving crude butadiene pre-separation technique of the invention will be then by that will generate the crude butadiene in gas
Pre-separation is carried out Deng the component of carbon four so that the component of the carbon such as most crude butadiene four is in stripper and crude butadiene knockout tower
In it is i.e. available by conventional distillation, the internal circulating load of the cyclic absorption oil of oily absorption and desorption workshop section is greatly reduced, so as to reduce
Public work consumption, saves energy consumption.In addition, crude butadiene separation column overhead need not be consumed than circulating cooling coolant-temperature gage more
The cold of low cryogen, saves power consumption.
(2) it is small to absorb oil loss：The present invention is separated using pre-separation+oily absorption and desorption technology, by will generate gas
In crude butadiene carry out pre-separation, a small amount of crude butadiene with generation gas go to carry out oily absorption and desorption, most cymogene two
Alkene and more heavy constituent carry out conventional distillation, and the heavy constituent pollution avoided in generation gas absorbs oil, greatly reduces and absorbs oil
Loss.
Brief description of the drawings
Fig. 1 is the schematic flow sheet of existing oily absorption and desorption technique；
Fig. 2 is a kind of schematic flow sheet of energy-saving crude butadiene pre-separation technique of the present invention；
In figure, T-1 is oil-absorption tower, and T-2 is desorber, and T-3 is solvent naphtha regenerator, and T-4 is stripper, and T-5 is thick
Butadiene pre-separation tower, E-1 compressors discharging cooler, E-2 is desorber input and output material heat exchanger, and E-3 is poor oil cooler, E-
4 be desorber condenser, and E-5 is desorption tower reboiler, and E-6 is solvent naphtha regenerator condenser, E-7 be solvent naphtha regenerator again
Device is boiled, E-8 is pre-separation tank feed cooler, and E-9 pre-separation tower reboilers, E-10 is pre-separation tower condenser, and E-11 is pre-
Knockout tower reboiler, E-12 are crude butadiene pre-separation tower feed heater, and V-1 is pre-separation tank, and C-1 is compressor.
Embodiment
The present invention is described in detail with specific embodiment below in conjunction with the accompanying drawings.
A kind of energy-saving crude butadiene pre-separation technique, as shown in Fig. 2 comprising the following steps：
(1) after the butylene oxidation-dehydrogenation reaction generation compressed coolings of gas S1, pre-separation tank V-1 separation is delivered to, wherein, tank deck
Gas phase S16 is sent into oil-absorption tower T-1 tower reactors, and the absorption oil S10 with entering from oil-absorption tower T-1 tower tops contacts absorption；
(2) S11 of oil-absorption tower top gaseous phase fixed gas one sends to exhaust gas processing device, and solution is sent into after tower reactor rich oil S4 heatings
Analyse in the middle part of tower T-2；
(3) S6 of gas phase fixed gas two of overhead extraction and butylene oxidation-dehydrogenation reaction generation gas S1 converges in Analytic Tower T-2
Recycle, be sent to after the oil-poor S8 coolings of tower reactor extraction at the top of oil-absorption tower T-1, side take-off crude butadiene S7 is sent to subsequently
BEU；
(4) pre-separation tank V-1 tank bottom liquid phases S17 is sent to stripper T-4, the top gas phase S18 produced at the top of stripper T-4
Converge with butylene oxidation-dehydrogenation reaction generation gas S1 and recycle, crude butadiene separation is sent to after tower reactor liquid phase S19 heat temperature raisings
Tower T-5；
(5) crude butadiene knockout tower T-5 overhead extraction crude butadiene S20 and Analytic Tower T-2 side take-offs crude butadiene
S7 mixing is latter with follow-up BEU is sent to, and tower reactor extraction heavy distillat S21 is discharged.
As a kind of preferred embodiment of the present invention, the oil-poor S8 and oil-absorption tower T-1 of the extraction of Analytic Tower T-2 tower reactors
The rich oil S4 of tower reactor exchanges heat in entry/exit material heat exchanger E-2 and realizes cooling respectively and heat up, and the extraction of Analytic Tower T-2 tower reactors
Oil-poor S8 is also cooled down after entry/exit material heat exchanger E-2 heat exchange coolings by poor oil cooler E-3.
As a kind of preferred embodiment of the present invention, described pre-separation tank V-1 operating pressure for 400kPa~
3000kPa, operation temperature are 273.15K~343.15K.It is furthermore preferred that described pre-separation tank V-1 operating pressure is
800kPa~1800kPa, operation temperature are 273.15K~313.15K.
As a kind of preferred embodiment of the present invention, the described pre-separation tank V-1 tank bottom liquid phases S17 component of carbon four
Mass percent concentration be 70.0~99.9wt%.It is furthermore preferred that the mass percent concentration of the described component of carbon four is
90.0~99.9wt%.
As a kind of preferred embodiment of the present invention, operating pressure in described stripper T-4 for 200kPa~
2000kPa, operation temperature are 273.15K~400.15K.It is furthermore preferred that the operating pressure in described stripper T-4 is
500kPa~1000kPa, tower reactor operation temperature are 313.15K~363.15K.
As a kind of preferred embodiment of the present invention, described crude butadiene knockout tower T-5 reflux ratio for 0.3~
2, operating pressure is 200kPa~1000kPa, and operation temperature is 273.15K~430K.It is furthermore preferred that described crude butadiene point
Reflux ratio from tower T-5 is 0.5~1.2, and operating pressure is 400kPa~800kPa.
Embodiment 1
The present invention is described by taking the flowsheeting result of calculation of 100,000 tons/year of Oxidative Dehydrogenation of Butene into Butadiene as an example.
Calculate underlying parameter explanation：
Carbon four loses：Constituent content≤0.1% of carbon four in oil-absorption tower T-1 top gas phases.
8000 hours operating times of year；
Compressor C-1 air inflows are 50.86 ton hours, and generation gas S1 feed compositions are shown in Table 1；
Table 1 generates gas composition (mass percent)
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 800kPaG, tower top temperature 282K, bottom temperature 343K；
Crude butadiene pre-separation tower T-5 operating pressure 400kPaG, tower top temperature 320K, bottom temperature 396K.
Technological process explanation：
Generation gas S1 (311K, 291kPaG) boosts to 1485kPaG by compressor C-1, obtains compressing unstripped gas S2, and
It is cooled to 276K in advance (i.e. through compressor discharging cooler E-1 (obtaining outlet material S3) and pre-separation tank feed cooler E-8 respectively
Material S15), initial gross separation is carried out subsequently into pre-separation tank V-1, tank deck gas phase S16 directly sends to oil-absorption tower T-1 tower reactors.
In oil-absorption tower T-1, tower reactor gas-phase feed (i.e. S16) contacts with tower top liquid phase scrubbing oil S10 cross-flows on column plate, by gas phase
The component of carbon four in charging absorbs.The S11 (1379kPaG, 30247kg/h) of oil-absorption tower T-1 top gaseous phases fixed gas one is sent
Remove exhaust gas processing device, the rich oil S4 (34795kg/h, 295K) and the oil-poor S8 of desorber T-2 tower reactors extraction of tower reactor
(28118kg/h, 415K) after heat exchange heating, obtains material S5 to be desorbed and sends to desorber T- in entry/exit material heat exchanger E-2
2 middle parts.The S6 of gas phase fixed gas two (740kg/h, 277K) of Analytic Tower T-2 overhead extractions returns to compressor C1 and with generating gas S1
Recycle together, side take-off crude butadiene S7 (5979kg/h, 315K) sends to the BEU in downstream, desorber
The oil-poor S8 of T-2 tower reactors extraction is absorbed after oily S23 converges with external complement forms oil-poor stock S9, is then changed respectively through entry/exit material
Hot device E-2, poor oil cooler E-3 are sent at the top of oil-absorption tower (i.e. tower top liquid phase scrubbing oil S10) after being cooled to 275K.Desorber
Condenser E-4 is condensed using cryogen, and cryogen can be chilled brine or propylene refrigerant, and Analytic Tower reboiler E-5 is steamed using low pressure
Vapour (1.3MPaG grades).
The pressured differences of pre-separation tank V-1 tank bottom liquid phase S17 are sent at the top of stripper T-4, the tower top of extraction at the top of stripper T-4
Gas phase S18 (325kg/h, 382K) returns to compressor C1 and converges and recycle together with generation gas S1, the liquid of tower reactor extraction
Phase S19 (14171kg/h, 344K) forms material flow S24 after the gasification of crude butadiene feed heater E-12 heating parts, and send
Go crude butadiene knockout tower T-5, crude butadiene knockout tower T-5 overhead extraction crude butadiene S20 (14050kg/h, 317K), tower reactor
Produce heavy distillat hydrocarbon S21 (121kg/h, 396K).The crude butadiene S7 of desorber T-2 side take-offs separates tower top with crude butadiene
Compound S22, which is formed, after the crude butadiene S20 mixing of extraction sends to BEU.Stripper reboiler E-9 and cymogene
Diene pre-separation tower feed heater E-12 is using the low grade residual heat of steam condensate or device remaining element as thermal source.Pre- point
Circulating cooling water cooling is used from tower condenser E-10, pre-separation tower reboiler E-11 then uses low-pressure steam (1.3MPaG etc.
Level) it is used as thermal source.
Comparative example 1
It is same as Example 1 to generate gas S1, difference is that comparative example 1 uses three traditional tower oil absorption and desorption techniques
Flow, as shown in figure 1, concrete technology explanation is：
Generation gas S1 boosts to obtain compression unstripped gas S2 by compressor C-1, and through compressor discharging cooler E-1 coolings
Outlet material S3 is obtained, is then fed into oil-absorption tower T-1.In oil-absorption tower T-1, tower reactor gas-phase feed (i.e. S16) and tower top
Liquid phase scrubbing oil S10 cross-flows on column plate are contacted, and the component of carbon four in gas-phase feed is absorbed.Oil-absorption tower T-1 tower tops
The S11 of gas phase fixed gas one sends to exhaust gas processing device, a part of oil-poor S8 of rich oil S4 and desorber T-2 the tower reactor extraction of tower reactor
In entry/exit material heat exchanger E-2 after heat exchange heating, obtain material S5 to be desorbed and send in the middle part of desorber T-2.Analytic Tower T-2
The S6 of gas phase fixed gas two of overhead extraction returns to compressor C1 and recycled together with generation gas S1, side take-off crude butadiene
S7 sends to the BEU in downstream, and a part of oil-poor S8 and the external complement of the extraction of desorber T-2 tower reactors absorb oil
S23, the oil-poor S13 of regeneration of solvent naphtha regenerator T-3 overhead extractions form oil-poor stock S9 after converging, then respectively through entry/exit material
Heat exchanger E-2, poor oil cooler E-3 are sent at the top of oil-absorption tower (i.e. tower top liquid phase scrubbing oil S10) after being cooled to 275K.Desorption
Tower T-2 overhead condensers E-4 is condensed using cryogen, and cryogen can be chilled brine or propylene refrigerant, and tower reactor reboiler E-5 is used
Low-pressure steam.
The oil-poor S12 of another part of Analytic Tower T-2 tower reactors extraction is sent into solvent naphtha regenerator T-3 regeneration, and in solvent naphtha
Regenerator T-3 overhead extractions regenerate oil-poor S13 and recycled, tower reactor extraction cut S14 discharges.Solvent naphtha regenerator condenser E-
6 are condensed using cryogen, and cryogen can be chilled brine or propylene refrigerant, and solvent naphtha regenerator reboiler E-5 uses low-pressure steam.
Traditional oily absorption and desorption technological process calculating parameter is as follows：
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 323K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 312K, bottom temperature 413K；
Solvent naphtha regenerator T-3 operating pressure 12kPaG, tower top temperature 360K, bottom temperature 387K.
For more traditional flow and the design energy consumption of the energy-saving crude butadiene separation process of the present invention, two kinds of flow meters
Calculate the generation gas index used and the crude butadiene index of total amount and side take-off is identical with total amount, and according to GB/T
50441-2007《Petrochemical industry designs energy consumption calculation standard》Energy conversion is carried out to electric power and power consumption working medium, reduced value is shown in Table
2, the design observable index of two kinds of technological processes is relatively shown in Table 3.
The electric power of table 2 and power consumption working medium energy reduced value
| Classification | Unit | Energy reduced value (MJ) |
| Electricity | kWh | 10.89 |
| Recirculated water | t | 4.19 |
| 1.3MPaG steam | t | 3349 |
3 two kinds of flow scheme design observable index of table are compared with (the unit interval：Hour)
As the data in table 3 indicates, in comprehensive energy consumption, because energy-saving crude butadiene separation process uses pre-separation technique,
Generate in gas about 30% C 4 materials to produce from pre-separation tank tank deck gas phase, about 70% C 4 materials are from pre-separation tank tank bottom
Liquid phase produces.Reach the same rate of recovery of carbon four, the absorption oil mass needed for energy-saving crude butadiene separation process separates for tradition
The 70% of oil mass is absorbed needed for flow.Comprehensive energy consumption reduces about 16.9% compared with traditional separation process.
On oil consumption is absorbed, because butylene oxidation-dehydrogenation reaction generates the aromatic hydrocarbons such as a small amount of benzene and toluene, for scale
It is annual to generate about 720 tons of the aromatic hydrocarbons such as benzene and toluene for 100,000 tons/year of device, if these heavy constituents are before oil-absorption tower
It is not isolated, can enters with the component of the carbon such as butadiene four and absorb in oil.And the absorption oil used in existing process is carbon
Six and the chain hydrocarbon mixture of carbon seven, carbon six and the chain hydrocarbon of carbon seven can and benzene, toluene etc. form azeotropic, it is impossible to divided using conventional distillation
From.With the increase for absorbing arene content in oil, absorbing the effect of oil can decline, and can finally take the mode changed and absorb oil,
The operating cost of device can so be increased.
Compared with traditional separation process, energy-saving crude butadiene pre-separation flow disappearing in steam, electricity and recirculated cooling water
It is less in consumption.By 0.3 yuan of recirculated water operating cost per ton, 1.3MPa steam per ton is worth 120 yuan, and power price is 0.6 yuan/
KWh, operating time in year are to be calculated for 8000 hours, can save 4,060,000 yuan of operating cost every year.
Embodiment 2
Compared with Example 1, the overwhelming majority is all identical, except in the present embodiment：
Pre-separation tank V-1 operating pressure is 400kPa, operation temperature 273.15K；
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 200kPaG, tower top temperature 273.15K, bottom temperature 313K；
Crude butadiene pre-separation tower T-5 operating pressure 200kPaG, reflux ratio 0.3, tower top temperature 273.15K, tower reactor temperature
Spend 380K.
Embodiment 3
Compared with Example 1, the overwhelming majority is all identical, except in the present embodiment：
Pre-separation tank V-1 operating pressure is 3000kPa, operation temperature 343.15K；
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 2000kPaG, tower top temperature 283K, bottom temperature 343.15K；
Crude butadiene pre-separation tower T-5 operating pressure 1000kPaG, reflux ratio 2, tower top temperature 385K, bottom temperature
430K。
Embodiment 4
Compared with Example 1, the overwhelming majority is all identical, except in the present embodiment：
Pre-separation tank V-1 operating pressure is 1000kPa, operation temperature 313.15K；
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 500kPaG, tower top temperature 313.15K, bottom temperature 335.2K；
Crude butadiene pre-separation tower T-5 operating pressure 600kPaG, reflux ratio 1.2, tower top temperature 290K, bottom temperature
360K。
Embodiment 5
Compared with Example 1, the overwhelming majority is all identical, except in the present embodiment：
Pre-separation tank V-1 operating pressure is 1800kPa, operation temperature 290K；
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 1000kPaG, tower top temperature 320.5K, bottom temperature 363.15K；
Crude butadiene pre-separation tower T-5 operating pressure 800kPaG, reflux ratio 0.5, tower top temperature 313.15K, tower reactor temperature
Spend 375.55K.
Embodiment 6
Compared with Example 1, the overwhelming majority is all identical, except in the present embodiment：
Pre-separation tank V-1 operating pressure is 1800kPa, operation temperature 290K；
Oil-absorption tower T-1 operating pressure 1379kPaG, tower top temperature 276K, bottom temperature 295K；
Desorber T-2 operating pressure 361kPaG, tower top temperature 314K, bottom temperature 413K；
Stripper T-4 operating pressure 1000kPaG, tower top temperature 320.5K, bottom temperature 363.15K；
Crude butadiene pre-separation tower T-5 operating pressure 800kPaG, reflux ratio 0.8, tower top temperature 313.15K, tower reactor temperature
Spend 375.55K.
The invention provides a kind of energy-saving crude butadiene pre-separation technique, has significant economic benefit.With reference to implementation
Example is illustrated, the personnel of association area can be carried out suitably changing or change according to method provided by the invention completely with
Combination, to realize the technology.It is it should be strongly noted that all these similar by being carried out to technological process provided by the invention
As change or change with reconfiguring, it is apparent to those skilled in the art, be considered as of the invention
In spirit, scope and content.
Claims (10)
1. a kind of energy-saving crude butadiene pre-separation technique, it is characterised in that comprise the following steps：
(1) after generating the compressed cooling of gas, the separation of pre-separation tank is delivered to, wherein, tank deck gas phase feeding oil-absorption tower tower reactor, and with
The absorption oil contact entered from oil-absorption tower tower top absorbs；
(2) oil-absorption tower top gaseous phase fixed gas one sends to exhaust gas processing device, is sent into after the heating of tower reactor rich oil in the middle part of Analytic Tower；
(3) the gas phase fixed gas two of overhead extraction converges and recycled with generation gas in Analytic Tower, the oil-poor cooling of tower reactor extraction
After be sent at the top of oil-absorption tower, side take-off crude butadiene is sent to follow-up BEU；
(4) pre-separation tank tank bottom liquid phase is sent to stripper, and the top gas phase of stripper top extraction is returned to converge with generation gas and followed
Ring is utilized, and crude butadiene knockout tower is sent to after the heating of tower bottoms heat phase；
(5) crude butadiene knockout tower overhead extraction crude butadiene mixes latter with being sent to the crude butadiene of Analytic Tower side take-off
Follow-up BEU, tower reactor extraction heavy distillat discharge.
2. a kind of energy-saving crude butadiene pre-separation technique according to claim 1, it is characterised in that Analytic Tower tower reactor is adopted
The oil-poor and rich oil of oil-absorption tower tower reactor gone out exchanges heat in entry/exit material heat exchanger and realizes cooling respectively and heat up, and Analytic Tower
Tower reactor produces oil-poor after the heat exchange cooling of entry/exit material heat exchanger, is also cooled down by poor oil cooler.
A kind of 3. energy-saving crude butadiene pre-separation technique according to claim 1, it is characterised in that described pre-separation
The operating pressure of tank is 400kPa~3000kPa, and operation temperature is 273.15K~343.15K.
A kind of 4. energy-saving crude butadiene pre-separation technique according to claim 3, it is characterised in that described pre-separation
The operating pressure of tank is 800kPa~1800kPa, and operation temperature is 273.15K~313.15K, the component of carbon four in tank bottom liquid phase
Mass percent concentration is 70.0~99.9wt%.
A kind of 5. energy-saving crude butadiene pre-separation technique according to claim 4, it is characterised in that carbon in tank bottom liquid phase
The mass percent concentration of four components is 90.0~99.9wt%.
A kind of 6. energy-saving crude butadiene pre-separation technique according to claim 1, it is characterised in that described stripper
Interior operating pressure is 200kPa~2000kPa, and operation temperature is 273.15K~400.15K.
A kind of 7. energy-saving crude butadiene pre-separation technique according to claim 6, it is characterised in that described stripper
Interior operating pressure is 500kPa~1000kPa, and tower reactor operation temperature is 313.15K~363.15K.
A kind of 8. energy-saving crude butadiene pre-separation technique according to claim 1, it is characterised in that described cymogene two
The reflux ratio of alkene knockout tower is 0.3~2, and operating pressure is 200kPa~1000kPa, and operation temperature is 273.15K~430K.
A kind of 9. energy-saving crude butadiene pre-separation technique according to claim 8, it is characterised in that described cymogene two
The reflux ratio of alkene knockout tower is 0.5~1.2, and operating pressure is 400kPa~800kPa.
A kind of 10. energy-saving crude butadiene pre-separation technique according to claim 1, it is characterised in that described generation
Gas is butylene oxidation-dehydrogenation reaction generation gas.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108218656A (en) * | 2018-01-08 | 2018-06-29 | 惠生工程（中国）有限公司 | A kind of separation method of the C_4 hydrocarbon containing light gas |
| CN110066212A (en) * | 2018-01-22 | 2019-07-30 | 惠生工程（中国）有限公司 | A kind of MTO technology by-product C 4 olefin oxidative dehydrogenation Butadiene Extraction Process |
| CN111825516A (en) * | 2019-04-19 | 2020-10-27 | 惠生工程（中国）有限公司 | Separation system and separation method of crude butadiene |
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| CN104418693A (en) * | 2013-09-02 | 2015-03-18 | 中国石化工程建设有限公司 | Energy-saving method of device for preparing butadiene by oxidative dehydrogenation of butene |
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| CN101353286A (en) * | 2007-07-25 | 2009-01-28 | 上海惠生化工工程有限公司 | Non-copious cooling lower carbon number hydrocarbons separation method containing light gas |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108218656A (en) * | 2018-01-08 | 2018-06-29 | 惠生工程（中国）有限公司 | A kind of separation method of the C_4 hydrocarbon containing light gas |
| CN108218656B (en) * | 2018-01-08 | 2021-06-29 | 惠生工程（中国）有限公司 | Method for separating carbon tetrahydrocarbon containing light gas |
| CN110066212A (en) * | 2018-01-22 | 2019-07-30 | 惠生工程（中国）有限公司 | A kind of MTO technology by-product C 4 olefin oxidative dehydrogenation Butadiene Extraction Process |
| CN110066212B (en) * | 2018-01-22 | 2022-04-01 | 惠生工程（中国）有限公司 | Process for preparing butadiene by oxidative dehydrogenation of carbon tetraolefin as byproduct in methanol-to-olefin process |
| CN111825516A (en) * | 2019-04-19 | 2020-10-27 | 惠生工程（中国）有限公司 | Separation system and separation method of crude butadiene |
| CN111825516B (en) * | 2019-04-19 | 2023-04-28 | 惠生工程（中国）有限公司 | Separation system and separation method of crude butadiene |
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